EP2082067A1 - Method and device for producing molten material - Google Patents
Method and device for producing molten materialInfo
- Publication number
- EP2082067A1 EP2082067A1 EP07818595A EP07818595A EP2082067A1 EP 2082067 A1 EP2082067 A1 EP 2082067A1 EP 07818595 A EP07818595 A EP 07818595A EP 07818595 A EP07818595 A EP 07818595A EP 2082067 A1 EP2082067 A1 EP 2082067A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- gas
- heat exchanger
- cooling
- heat
- top gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
- C21B13/143—Injection of partially reduced ore into a molten bath
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/14—Multi-stage processes processes carried out in different vessels or furnaces
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B13/00—Making spongy iron or liquid steel, by direct processes
- C21B13/0006—Making spongy iron or liquid steel, by direct processes obtaining iron or steel in a molten state
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
- C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
- C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/40—Gas purification of exhaust gases to be recirculated or used in other metallurgical processes
- C21B2100/44—Removing particles, e.g. by scrubbing, dedusting
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21B—MANUFACTURE OF IRON OR STEEL
- C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
- C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
- C21B2100/66—Heat exchange
-
- C—CHEMISTRY; METALLURGY
- C21—METALLURGY OF IRON
- C21C—PROCESSING OF PIG-IRON, e.g. REFINING, MANUFACTURE OF WROUGHT-IRON OR STEEL; TREATMENT IN MOLTEN STATE OF FERROUS ALLOYS
- C21C2100/00—Exhaust gas
- C21C2100/06—Energy from waste gas used in other processes
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/10—Reduction of greenhouse gas [GHG] emissions
- Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P10/00—Technologies related to metal processing
- Y02P10/25—Process efficiency
Definitions
- the invention relates to a method for producing molten metal, wherein oxygen, reducing agent and in a reduction reactor reduced iron are introduced into a melter gasifier, the reducing agent gasified with the oxygen and the resulting heat, the reduced iron is melted, the dome gas from the A melt gasifier is used as at least a portion of the reducing gas, and wherein reacted top gas is withdrawn from the reduction reactor, and a plant for carrying out the method, with one or more reducing reactors with reducing gas, a melt gasifier with oxygen supply and a supply system for reducing agent, at least one line for the supply of the dome gas from the melt gasifier in the reduction reactor and at least one line for the removal of the top gas from the reduction reactor.
- oxygen is injected at a temperature of 25 ° C and a purity of ⁇ 95% by volume via the nozzles in the melter gasifier to gasify the reducing agent (mainly coal and coal briquettes) and to provide the required heat for the melting of the reduced iron.
- the dome gas of the melter gasifier is used for indirect reduction in a fixed bed reduction shaft (FBRS) or in fluidized bed reactors (ESC), after which it is withdrawn as top gas.
- the purified export gas which is composed of the top gas from the direct reduction unit and the dome gas from the melter gasifier, has the following typical analysis at 1.5 barg: CO 45% by volume, CO 2 30% by volume, H 2 19% by volume, H 2 O 3 vol% and N 2 3 vol%. Due to the excess gas, it must be recycled and optimized for total energy.
- top gas or export gas of smelting reduction plants contains large amounts of sensible heat (top gas temperatures are around 250 ° C-500 ° C), but also the portion of the reducing gas, which is not introduced into the reduction reactor, but as excess gas for the pressure control
- the temperature of the reducing gas is about 700 0 C - 900 0 C.
- export gas in a power plant (steam power plant or gas and steam power plant) or for metallurgical use (eg Direct reduction plant)
- the gas must be free from the impurities (dust, tar) getting cleaned.
- wet scrubbers are usually used today, which simultaneously cool the gas to about 40-45 0 C and thereby extract the gas from the majority of the sensible heat. The heat is dissipated by the process water and indicated by cooling towers to the environment.
- the object of the present invention was therefore to provide a method or a system as described above, with increased energy and raw material efficiency.
- the method according to the invention is characterized in that at least a portion of the heat energy of the top gas and / or intended for use as a cooling gas and excess gas portion of the reducing gas for indirect heating of at least one further gas used in the process is used.
- At least part of the top gas is returned to the reduction reactor after at least one cooling or cleaning and a heat exchange with the hot process gas.
- the cleaning takes place by means of wet scrubbing. This allows simultaneous cooling or cleaning.
- the recycled, heated top gas is added to the dome gas and fed together with this the reduction reactor, preferably particulate ingredients are deposited before entering the reduction reactor from the gas mixture.
- At least a portion of the top gas after at least one cooling or cleaning, and heat exchange with the top gas and / or provided for use as a cooling gas and excess gas portion of the reducing gas are introduced into the melter gasifier. Due to the heating of the gas recirculated into the melt gasifier, higher injection rates of top gas, recirculated product gas from a CO 2 Entfemungsstrom (eg pressure change system, amine scrubbing, Benfield laundry, etc.), from a fine coal injection or Kunststoffindüsung, etc. possible because the heating is a compensation for the per se by the injection reduced adiabatic flame temperature (RAFT).
- RAFT injection reduced adiabatic flame temperature
- the recirculated top gas is advantageously compressed before the heat exchange and / or its carbon dioxide content after cooling, preferably to 30 to 50 0 C, reduced, preferably to 2 to 3% by volume.
- a further variant of the method according to the invention is characterized in that the heat energy of the top gas and / or the intended use of the cooling gas and excess gas portion of the reducing gas is used for heating the oxygen for the melter gasifier.
- the heat released by the gasification of the coal, coal briquettes and optionally coke with oxygen is required for calcining the aggregates, for heating the fixed bed in the melter gasifier (coal, coal briquettes, DRI, aggregates) and for melting the DRI.
- the higher temperature of the oxygen which is blown into the melter gasifier via the nozzles or via the dust burners results in a lower consumption of reducing agent and therefore a saving of coal and coal briquettes as reducing agent.
- the amount of oxygen can also be reduced.
- the preheating of the oxygen also enables higher injection rates of top gas, recirculated product gas from a CO 2 removal plant, a fine coal injection or plastic injection, etc., and in combination with the return of heated top gas or product gas produced therefrom into the melter gasifier - Amount of top gas or product gas, etc. are maximized.
- the heat exchange takes place between the top gas and / or the proportion of the reducing gas and the oxygen intended for use as cooling gas and excess gas via a carrier medium and two heat exchange processes.
- a carrier medium and two heat exchange processes preferably waste N 2 or water vapor is used.
- the carrier medium can be used after heat exchange with the oxygen, possibly together with a partial flow of the uncooled carrier medium for preheating required in the process combustion gas.
- the heat energy of the top gas and / or of the proportion of the reducing gas intended for use as cooling gas and as excess gas is used to generate steam.
- the heat energy of the steam is used to heat the oxygen for the melter gasifier.
- the system described above is inventively to solve the task characterized by at least one heat exchanger in a line for the removal of the top gas and / or in the cooling gas and excess gas system, which heat exchanger is flowed through by at least one further gas used in the process.
- the cooling gas and excess gas system is to be understood as meaning the line system through which the fraction of the reducing gas intended for use as cooling gas and as excess gas flows after its separation from the reducing gas stream conducted into the reduction reactor.
- the cleaning unit is designed as a wet scrubber, so that can be cooled and cleaned at the same time.
- the or each heat exchanger is designed as a tube heat exchanger or tube bundle heat exchanger, and flows through from top to bottom of the top gas.
- a further embodiment of the invention is after the cooling and cleaning unit for the top gas from a return line for the top gas and leads to the heat exchanger, and leads the return from the heat exchanger to the reduction reactor.
- the return line from the heat exchanger opens into the connecting line between the melt gasifier and reduction reactor for the dome gas, preferably in front of any particle separator.
- Another embodiment of the invention is characterized in that after the cooling and cleaning unit, a return line for the top gas emanates and leads to the heat exchanger, and that the return line from the heat exchanger further leads to the melt gasifier, preferably to the mouth of the oxygen supply parallel thereto.
- Heat exchanger a compressor, if necessary, a cooling device and a
- Carbon dioxide reduction stage are used, wherein the output of the compressor and the output of the carbon dioxide reduction stage in a common supply line lead to the heat exchanger.
- the system is advantageously designed such that in the oxygen supply to the melt gasifier, a further heat exchanger is used, with at least one of the top gas and / or the for use as a cooling gas and provided as the excess gas portion of the reducing gas flows through a heat exchanger of a heat transfer fluid, preferably in liquid and / or vapor form, flows through the circle.
- At least one further heat exchanger for at least one combustion gas required in the process is arranged in the circuit of the heat transfer fluid.
- a reduction shaft 1 is of lumpy or pellet-shaped iron ore, optionally supplied with unburned aggregates.
- discharge devices 2 the sponge iron produced in the reduction shaft 1 and the partially calcined (calcined) aggregates are introduced into the head of a melter gasifier 3.
- Liquid pig iron collects at the bottom of the melter gasifier 3 and above it liquid slag, which is preferably drawn off discontinuously via taps.
- the gasifier 3 is fed to the melter gasifier 3, preferably coal or coal briquettes possibly mixed with sieved undersize of the iron ore, otherwise for the Reduction process could not be used.
- an oxygen-containing gas is supplied in the lower region of the melter gasifier 3.
- the reducing gas produced is led out of the top of the melter gasifier 3 via a line 6, freed of solid constituents, in particular dust and fine-grained pyrolyzed coal, in a hot gas cyclone 7 and then passes via a line 8 into the reduction shaft 1.
- the reducing gas flows through the latter the bed of iron ore and aggregates in countercurrent, thereby reducing the iron ore to sponge iron and partially calcined the aggregates.
- the separated in the hot gas cyclone 7, pyrolized pulverized coal and other particulate ingredients are returned to the melter gasifier 3, preferably when entering this by arranged in the wall of the melter gasifier 3 dust burner, which also oxygen-containing gas is fed, gasified.
- the at least partially consumed reducing gas is withdrawn at the upper end of the reduction shaft 1 via a top gas line 9 and fed to the cleaning unit 10 as export gas due to the excess gas utilization and total energy optimization.
- a portion of the reducing gas is used for pressure control of the plant and as a cooling gas. This portion of the reducing gas is separated by the line 23 from the guided into the reduction shaft 1 reducing gas stream. The line 23 is thus the first part of the cooling gas and excess gas system.
- the reducing gas used to control the pressure of the plant, called reducing gas is mixed after the cooling and cleaning unit 11 the export gas.
- the reducing gas used as the cooling gas is recycled after the cooling and cleaning unit 11 and compression in the compressor 24 via the line 12 in the line 6 in front of the hot gas cyclone 7.
- the export gas In order to make the export gas usable in an energy-optimized manner for the process itself and preferably to use at least a portion of the reduction gas required in the reduction shaft 1, at least a portion of the export gas via behind the cleaning unit 10 via a line 13 by means of a compressor 14 with a possible high suction pressure branched off and compressed. At best, also excess gas can be diverted and recycled behind the cooling and cleaning unit 11 via a further line before the admixture to the export gas.
- the recirculated export gas is taking advantage of the energy content of the directly withdrawn from the reduction shaft 1 top gas, which has a temperature between about 25O 0 C and 500 0 C, from a temperature after the cooling and cleaning unit of about 4O 0 C up to about 400 0 C heated.
- a heat exchanger 15 is used in the line 9 for the top gas before the cleaning unit 10, which is also traversed by the branched off via the line 13 portion of the export gas.
- the heated export gas is fed into the duct 6 for the dome gas of the melter gasifier 3, before the hot gas cyclone 7.
- the process improved in this way has increased energy efficiency due to lower process water quantities required for cooling the top gas, which also means a reduction in the energy requirement for the process water pumps.
- the heat dissipated by the top gas into the process water is reduced, which is lost through cooling towers or causes evaporation through water loss in the system, which must be constantly balanced.
- the heat exchanger 15 At most, at least a portion of the diverted via the line 13 export gas after intermediate cooling to 30-50 0 C in the cooler 16 and reduction of CO 2 content to 2-3% by volume in the system 17 for CO 2 removal the heat exchanger 15 is supplied become. Also, the cooled and CO 2 -reduced gas could be mixed with untreated recycle gas prior to entering the heat exchanger 15, allowing precise adjustment of temperature and / or CO 2 content in the recycle gas.
- the recirculated top gas can also be introduced into the melter gasifier 3 after passing through the heat exchanger 15, preferably via lances introduced into the oxygen nozzles, the return line for the top gas extending parallel to the mouth of the oxygen feed 5.
- the recirculated top gas does not have to be heated by a reduction gas furnace, electric heater or plasma torch using external energy in this case, but it is the thermal energy of the top gas before the cleaning unit 10 exploited. This results in the above-mentioned advantages of increasing the energy efficiency of the process, lower process water required for cooling the top gas, reducing the energy requirement of the process water pumps, and reducing the heat dissipated by the top gas into the process water, which is lost through cooling towers or water loss through evaporation in the system causes.
- a heat exchanger 18 may be inserted into the line 9 for the top gas before the cleaning unit 10, which is traversed by a heat transfer medium such as waste N 2 .
- the heat exchanger 18 forms together with another heat exchanger 19 a circuit for the heat transfer medium.
- the heat exchanger 19 is preferably passed through a gas to be supplied to the melter gasifier 3, preferably through the oxygen to be injected, which gas is thus heated indirectly and with the highest possible degree of safety due to non-reactive pairing of, for example, oxygen with the heat transfer medium by the energy content of the top gas.
- the preheating of the oxygen also enables higher injection rates of top gas, recirculated product gas from a CO 2 removal plant, fine coal injection or plastic injection, etc., and in combination with the return of heated top gas into the melter gasifier, the recirculation amount of top gas or gas can be increased PSA product gas or its injection rates can be maximized.
- the energy of the top gas receiving heat transfer fluid 20 may be used in which combustion air or drying medium, for example air, N 2 , exhaust gas, od. Like., For an ore and / or coal dryer is heated. This can also be used to save fuel here.
- a heat exchanger 21 through which steam flows as the heat transfer fluid is conceivable as an alternative embodiment of the system.
- This heat exchanger 21 then forms a circuit in a similar manner as described above, together with a further heat exchanger 22, wherein here too the heat exchanger 22 is preferably flowed through by a gas to be fed to the meltdown gasifier 3.
- the flow through the top gas heat exchanger 15, 18 and 21 are preferably designed as a pipe or shell and tube heat exchanger, which is still conducted before the cleaning unit 10 still contaminated top gas in a vertical direction from top to bottom to avoid dust deposits.
- the heat exchanger 15, 18 or 21 or additional heat exchangers could also be used in the cooling gas and excess gas system, which by slightly lower gas volumes, but higher temperatures of about. 750 0 C to 850 0 C is characterized.
- a bypass line can be provided around the heat exchangers 15, 18, 21 both in the top gas system and in the cooling gas and excess gas system.
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102006048600A DE102006048600B4 (en) | 2006-10-13 | 2006-10-13 | Method and device for producing molten material |
PCT/EP2007/008515 WO2008046504A1 (en) | 2006-10-13 | 2007-10-01 | Method and device for producing molten material |
Publications (2)
Publication Number | Publication Date |
---|---|
EP2082067A1 true EP2082067A1 (en) | 2009-07-29 |
EP2082067B1 EP2082067B1 (en) | 2012-04-04 |
Family
ID=38924525
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP07818595A Not-in-force EP2082067B1 (en) | 2006-10-13 | 2007-10-01 | Method and device for producing molten material |
Country Status (18)
Country | Link |
---|---|
US (1) | US8317898B2 (en) |
EP (1) | EP2082067B1 (en) |
JP (1) | JP2010506047A (en) |
KR (1) | KR101424166B1 (en) |
CN (1) | CN101636510B (en) |
AR (1) | AR064592A1 (en) |
AT (1) | ATE552356T1 (en) |
AU (1) | AU2007312666B2 (en) |
BR (1) | BRPI0719882B1 (en) |
CA (1) | CA2665770C (en) |
CL (1) | CL2007002940A1 (en) |
DE (1) | DE102006048600B4 (en) |
MX (1) | MX2009003732A (en) |
RU (1) | RU2453609C2 (en) |
TW (1) | TW200825183A (en) |
UA (1) | UA94623C2 (en) |
WO (1) | WO2008046504A1 (en) |
ZA (1) | ZA200902092B (en) |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
AT507003B1 (en) | 2008-06-27 | 2010-03-15 | Siemens Vai Metals Tech Gmbh | PROCESS GAS CLEANING DEVICE FOR A MELT REDUCTION PLANT FOR THE COLLECTION OF RAW IRON |
AT507113B1 (en) * | 2008-07-17 | 2010-07-15 | Siemens Vai Metals Tech Gmbh | METHOD AND APPARATUS FOR ENERGY AND CO2 EMISSION OPTIMIZED IRON PRODUCTION |
AT507823B1 (en) * | 2009-01-30 | 2011-01-15 | Siemens Vai Metals Tech Gmbh | METHOD AND APPARATUS FOR PRODUCING RAW IRONS OR LIQUID STEEL PREPARED PRODUCTS |
AT507955B1 (en) | 2009-02-20 | 2011-02-15 | Siemens Vai Metals Tech Gmbh | METHOD AND APPARATUS FOR MANUFACTURING SUBSTITUTE GAS |
AT509073B1 (en) * | 2009-12-23 | 2011-06-15 | Siemens Vai Metals Tech Gmbh | METHOD AND DEVICE FOR PROVIDING REDUCTION GAS FROM GENERATOR GAS |
AT509865B1 (en) * | 2010-04-26 | 2011-12-15 | Siemens Vai Metals Tech Gmbh | METHOD FOR THE PRODUCTION OF RAW IRONS OR LIQUID STEEL PREPARED PRODUCTS |
AT511243B1 (en) * | 2011-03-17 | 2013-01-15 | Siemens Vai Metals Tech Gmbh | HÜTTENTECHNISCHE ANLAGE WITH EFFICIENT DOWNWATER USE |
US20150259760A1 (en) * | 2012-09-14 | 2015-09-17 | Voestalpine Stahl Gmbh | Method for producing steel |
DE102013015019A1 (en) * | 2013-09-10 | 2015-03-12 | Bogdan Vuletic | Process and plant for the gasification of carbon carriers and further processing of the produced gas |
CN109318416A (en) * | 2018-10-25 | 2019-02-12 | 周军 | A kind of safe plastic bucket compacting Casting Equipment |
CN115652008B (en) * | 2022-09-23 | 2023-11-21 | 山东祥桓环境科技有限公司 | High-temperature carbon-rich reforming system and process for smelting reducing gas |
Family Cites Families (14)
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US1996558A (en) * | 1930-04-15 | 1935-04-02 | Schering Kahlbaum Ag | Production of terpenes |
JPS5029414B1 (en) * | 1970-12-28 | 1975-09-23 | ||
DE2843303C2 (en) * | 1978-10-04 | 1982-12-16 | Korf-Stahl Ag, 7570 Baden-Baden | Process and plant for the production of liquid pig iron and reducing gas in a melter gasifier |
AT360567B (en) * | 1979-05-18 | 1981-01-26 | Voest Alpine Ag | METHOD FOR OVERCOMING MALFUNCTIONS IN THE CONTINUOUS DIRECT REDUCTION OF IRON ORE AND PLANT THEREFOR |
IN158544B (en) * | 1982-11-15 | 1986-12-06 | Korf Engineering Gmbh | |
US4685964A (en) * | 1985-10-03 | 1987-08-11 | Midrex International B.V. Rotterdam | Method and apparatus for producing molten iron using coal |
DE4240197C2 (en) * | 1992-11-30 | 1996-04-18 | Vuletic Bogdan Dipl Ing | Process for the production of pig iron from iron ore and device for the thermal and / or chemical treatment of a readily disintegrating material or for the production of pig iron by means of this process |
US5643354A (en) * | 1995-04-06 | 1997-07-01 | Air Products And Chemicals, Inc. | High temperature oxygen production for ironmaking processes |
US5582029A (en) * | 1995-10-04 | 1996-12-10 | Air Products And Chemicals, Inc. | Use of nitrogen from an air separation plant in carbon dioxide removal from a feed gas to a further process |
AT406964B (en) * | 1998-03-11 | 2000-11-27 | Voest Alpine Ind Anlagen | METHOD FOR THE PRODUCTION OF LIQUID PIG IRON AND / OR STEEL PRE-PRODUCTS |
AT409634B (en) * | 2000-05-15 | 2002-09-25 | Voest Alpine Ind Anlagen | METHOD AND DEVICE FOR THE PRODUCTION OF RAW IRON OR LIQUID STEEL PRE-PRODUCTS FROM IRON-CONTAINING MATERIALS |
JP3939492B2 (en) * | 2000-11-08 | 2007-07-04 | 株式会社神戸製鋼所 | Coal gasification direct reduction iron making |
RU2272849C1 (en) * | 2004-07-19 | 2006-03-27 | Валентин Павлович Цымбал | Method of production of metals from ore materials and unit for realization of this method |
EP1826281A1 (en) * | 2006-02-24 | 2007-08-29 | Paul Wurth S.A. | Method for producing molten pig iron or steel pre-products in a melter gasifier |
-
2006
- 2006-10-13 DE DE102006048600A patent/DE102006048600B4/en not_active Expired - Fee Related
-
2007
- 2007-10-01 BR BRPI0719882A patent/BRPI0719882B1/en not_active IP Right Cessation
- 2007-10-01 RU RU2009117816/02A patent/RU2453609C2/en not_active IP Right Cessation
- 2007-10-01 EP EP07818595A patent/EP2082067B1/en not_active Not-in-force
- 2007-10-01 UA UAA200903420A patent/UA94623C2/en unknown
- 2007-10-01 WO PCT/EP2007/008515 patent/WO2008046504A1/en active Application Filing
- 2007-10-01 AU AU2007312666A patent/AU2007312666B2/en not_active Ceased
- 2007-10-01 CN CN2007800376446A patent/CN101636510B/en not_active Expired - Fee Related
- 2007-10-01 JP JP2009531735A patent/JP2010506047A/en active Pending
- 2007-10-01 CA CA2665770A patent/CA2665770C/en not_active Expired - Fee Related
- 2007-10-01 AT AT07818595T patent/ATE552356T1/en active
- 2007-10-01 KR KR1020097009817A patent/KR101424166B1/en active IP Right Grant
- 2007-10-01 MX MX2009003732A patent/MX2009003732A/en unknown
- 2007-10-01 US US12/445,358 patent/US8317898B2/en not_active Expired - Fee Related
- 2007-10-01 ZA ZA200902092A patent/ZA200902092B/en unknown
- 2007-10-03 TW TW096136998A patent/TW200825183A/en unknown
- 2007-10-12 AR ARP070104523A patent/AR064592A1/en unknown
- 2007-10-12 CL CL200702940A patent/CL2007002940A1/en unknown
Non-Patent Citations (1)
Title |
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See references of WO2008046504A1 * |
Also Published As
Publication number | Publication date |
---|---|
CA2665770C (en) | 2014-08-05 |
BRPI0719882A2 (en) | 2014-04-29 |
EP2082067B1 (en) | 2012-04-04 |
RU2453609C2 (en) | 2012-06-20 |
ZA200902092B (en) | 2010-06-30 |
KR101424166B1 (en) | 2014-08-01 |
TW200825183A (en) | 2008-06-16 |
RU2009117816A (en) | 2010-11-20 |
US20100043599A1 (en) | 2010-02-25 |
AU2007312666B2 (en) | 2011-07-14 |
DE102006048600B4 (en) | 2012-03-29 |
KR20090080965A (en) | 2009-07-27 |
AU2007312666A1 (en) | 2008-04-24 |
CN101636510A (en) | 2010-01-27 |
CA2665770A1 (en) | 2008-04-24 |
BRPI0719882B1 (en) | 2016-02-10 |
AR064592A1 (en) | 2009-04-15 |
JP2010506047A (en) | 2010-02-25 |
MX2009003732A (en) | 2009-04-22 |
DE102006048600A1 (en) | 2008-04-17 |
UA94623C2 (en) | 2011-05-25 |
CN101636510B (en) | 2012-05-16 |
WO2008046504A1 (en) | 2008-04-24 |
US8317898B2 (en) | 2012-11-27 |
ATE552356T1 (en) | 2012-04-15 |
CL2007002940A1 (en) | 2008-05-30 |
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